Note : Les descriptions sont présentées dans la langue officielle dans laquelle elles ont été soumises.
CA 02819411 2015-01-15
Integrated Process for Upgrading Heavy Oil
FIELD OF THE TECHNOLOGY
[0001] The invention relates to an integrated process for deeply upgrading of
heavy oil, in
particular to an integrated process for producing high-quality upgraded oil,
including
prefractionation of heavy crude oil, extra heavy crude oil and oil sand
bitumen, heavy-fraction
deasphalting process, thermal crooking process and fixed-bed hydrotreating
process. The
integrated process belongs to the heavy oil processing field.
BACKGROUND
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[0002] Heavy oil is the petroleum with API gravity lower than 20 (its density
is higher than 0.932
g/cm3 at the temperature of 20 C) , generally comprising heavy crude oil, oil
sand bitumen and
residue. As the heavy crude oil and the oil sand bitumen have high density,
high viscosity and high
freezing point, they will lose flowability at ambient temperature or even
higher temperature, and
cannot be transported and processed like conventional crude oil. Particularly,
the extra heavy oil and
the oil sand bitumen with API gravities lower than 10 need to be blended with
diluent or to be
converted to light fraction, so as to form synthetic oil, which is then
transported to a refinery to be
processed. Therefore, the research and development of light fraction
conversion and processing
technology for the heavy oil is always a topic attracting wide interest in the
industry.
[0003] One of the most important technologies of the heavy oil processing is
the secondary
upgrading for oil products. With the thermal reaction treatments of heavy oil
components, for
example, heavy oil hydrotreating, the hydrotreating of coking products,
partial thermal cracking of
heavy distillate products, etc., the upgraded products of the heavy oil
(upgraded oil or synthetic oil)
can be obtained. The secondary upgrading is beneficial for solving the
stability problem of the
thermal reaction products and removing impurities (such as sulfur and so on)
in crude oils, thus
obtaining the synthetic oil being more clean and stable and with increased APT
gravity. The
upgraded oil or the synthetic oil has good flowability, which can be easily
transported to a refinery;
in addition, the impurities, asphaltenes, metals and carbon residue precursors
in the treated upgraded
oil are removed significantly, thus improving the quality of the oil and also
convenient for the
subsequent oil processing.
[0004] The key heavy components influencing the quality of the heavy oil are
asphaltenes and
metals, therefore, the deasphalting process is also an important step for
converting the heavy oil to
light oil. As for the heavy oil process, the de-asphalted oil with good
properties can be obtained from
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the heavy oil through a solvent deasphalting process. However, the selection
of the extraction
solvent and the determination of the operating parameters for extraction
process are greatly
restricted by the properties of asphalt, which has the characteristics of high
softening point, high
viscosity and easily forms coke by heating. The existing problems firstly are
that the asphalt with
high softening point and the solvent are difficult to be separated that it is
difficult to increase yield of
de-asphalted oil, and secondly are that hard asphalt is difficult to be
transported because of its high
viscosity and easily forms coke by heating. Under the restrictions of these
technical problems, the oil
yield of the 'de-asphalted oil process for heavy oil, extra heavy oil and oil
sand bitumen is low and a
large quantity of asphalt needs to be processed or utilized in other proper
ways, during the solvent
deasphalting process currently.
[0005] In order to improve the heavy oil processing, combined processes with
various matching
designs are disclosed and utilized. Their purposes are all that: through more
than two combined
treatment processes, the heavy oil is processed and upgraded more effectively,
improving its API
gravity and producing the corresponding upgraded oil (it is also called as
synthetic oil). En some
combined processes, the de-asphalted oil and de-oiled asphalt are obtained
through the solvent
deasphalting process, which is a necessary process for various combined
processes, such as the
combined process of the solvent deasphalting process and delayed coking
process, the combined
process of the solvent deasphalting process and hydrotreating process, and so
on, For example,
Europe Patent No, EP1268713(A1) discloses a process for upgrading heavy oil
feedstock. By using
the solvent deasphalting process, the de-asphalted oil and the de-oiled
asphalt are obtained and
respectively. subjected to slurry-bed hydrocracking. The upgraded oil and the
unreformed asphalt are
separated from hydrotreating products. The asphalt with the boiling point more
than 1025 F can be
taken as coked feedstock and PDX gasification feedstock. US patent No.
6,673,234 discloses a
combined process of initial solvent deasphalting process followed by delayed
coking process. After
the residual oil is treated in the solvent deasphalting process, the de-
asphalted oil obtained is
processed in the delayed coking, which can lengthen coking cycle time and
produce needle coke. In
the combined process, which has been used or disclosed, involving solvent
deasphalting processes, it
is necessary to separate the solvent in the de-oiled asphalt. That is, solvent
needs to be separated
from de-oiled asphalt firstly and, then, the de-oiled asphalt enters the
sequent combined process.
Therefore, the two problems associated with the asphalt with high softening
point and the solvent
are difficult to be separated from each other during the solvent deasphalting
process and the asphalt
with high softening point is hard to be transported are not solved. On the
other hand, currently, as for
the heavy oil process technology, the difficulty of the separation of the de-
oiled asphalt from the
solvent is reduced at the cost of lowering the yield of de-asphalted oil, thus
increasing the quantity of
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de-oiled asphalt. As the oil component in the asphalt is relatively high, the
quantity of coke produced
in cocking process after the thermal reaction of the asphalt is also
increased; that is, the amount of
the coke and the gas are difficult to be decreased. Still on the other hand,
in order to reduce the
difficulty of separation of solvent from the asphalt with high softening point
and the difficulty of
transporting of the asphalt with high softening point, the oil component
residues in the de-oiled
asphalt is relatively high. During the thermal cracking process, part of the
oil component undergoes
condensation reaction, and then the quantity of coke in the thermal reaction
is necessarily increased,
thus influencing not only the liquid yield but also the stability of the
upgraded products.
SUMMARY
[0006] The main technical problem that the invention solves is to provide an
integrated process for
processing heavy oil. Through prefractionation of the heavy oil in combination
with a solvent
deasphalting process and an asphalt thermal cracking process, the extraction
solvent used for
deasphalting and the heavy gas oil separated from the asphalt thermal cracking
reaction are
respectively recycled back to the solvent deasphalting process, thus forming a
bidirectional
integrated process, which overcomes the defect that the de-oiled asphalt is
difficult to separate from
solvent in the prior art, and the oil component can be extracted in the heavy
oil without the need
of thermal reaction treatment, thereby guaranteeing the stability of the
upgraded products and also
increasing the yield of liquid and upgraded oil.
[0007] The invention also provides upgraded oil product from a heavy oil
process. The upgraded
oil product is obtained from processing heavy oil according to the integrated
process of the invention
and combining the oil components produced during respective processes, wherein
the impurities
including metal, asphaltenes and so on and coke forming precursors are
separated from each other to
the maximum extent. In additions, the oil components produced via physical
separation have high
hydrogen content and the products have good stability.
[0008] One aspect of the invention provides a integrated process for
processing heavy oil,
comprising at least the following processes:
[0009] heavy oil, which substantially does not comprise <350 C atmospheric
distillates, is used as
feed for solvent deasphalting process in an extraction tower together with
extraction solvent,
collecting de-asphalted oil and de-oiled asphalt phase including the
extraction solvent;
[0010] the de-oiled asphalt phase including the extraction solvent is mixed
with dispersing solvent
and then enters a thermal cracking reactor to undergo thermal cracking
process, so as to obtain
thermal cracking reaction products and coke, leading out of the thermal
cracking reaction products,
separating, the solvent, thermal cracking oil and 450 C+heavy gas oil;
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[0011] the solvent separated from the thermal cracking products is recycled
back to the solvent
deasphalting process, 450 C + heavy gas oil is recycled back to the solvent
deasphalting process and
taken as mixed feed with heavy oil;
[0012] upgraded oil is obtained through the mixture of the de-asphalted oil
and the thermal
cracking oil separated from the thermal cracking reaction products.
[0013] The heavy oil feedstock in the invention is mainly heavy crude oil
(including extra heavy
oil) with API gravity less than 20 (its density under the temperature of 20 C
is higher than
0.932g/cm3) or oil sand bitumen, all of these materials can be used as the
feedstock for the integrated
process without limiting to any particular production method of the feedstock.
The integrated
process at least comprises a solvent deasphalting process of the oil feedstock
and a thermal cracking
process of a de-oiled asphalt phase. In addition, the bidirectional integrated
process is realized
through the recycle of the extraction solvent and thermal cracking heavy oil.
[0014] According to the integrated process in the invention, in order to
produce upgraded oil and
improve its quality to the maximum extent and hence increase the proportion of
straight-run
distillation component in the upgraded oil, the integrated process can also
include distillation and
separation Process for the oil feedstock. When boiling range of the
distillates included in the oil
feedstock is relatively wide, prefractionation can be conducted to separate
the straight-run distillate
oil. And then the oil components are separated to the maximum extent through
solvent extraction
deasphalting and thermal cracking of de-oiled asphalt containing the solvent.
With the process, the
oil components which can be extracted from the heavy oil do not need to be
subjected to the thermal
reaction, thus removing undesired components to the maximum extent while also
improving the
stability of the upgraded products.
[0015] Specifically, the integrated process in the invention can also
comprise: the heavy oil
including <350 C atmospheric distillates are firstly subjected to
prefractionation by distillation;
collecting distillate oil, and the products from the bottom of the tower is
fed to the de-asphalting
process, the temperature of the cut point of the prefractionation is 350-565
C. The obtained
distillate oil is mixed with the de-asphalted oil and thermal cracking oil so
as to form the upgraded
oil, or the obtained distillate oil is taken as light oil to be processed to
be independently processed in
the sequent processes. The prefractionation can comprise atmospheric
distillate process or
atmospheric plus vacuum distillate process. According to the properties of the
oil feedstock and
product requirements, the distillation cut point can be controlled and one or
a plurality number of
distillate oils can be obtained.
[0016] According to the integrated process in the invention, distillate oil,
de-asphalted oil and
thermal cracking heavy gas oil , which are produced in various stages of the
process, can be mixed
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and allocated according to the needed proportion, thus realizing the flexible
adjustment of the
upgraded oil which is used as feedstock for downstream processing.
Particularly, the upgraded oil is
further processed with fixed-bed hydrotreating process and hydrotreating
upgraded oil can be
obtained.
[0017] According to embodiments of the integrated process in the invention,
two extraction steps
can be carried out in the solvent deasphalting process; that it, firstly, a
first extraction solvent (it is
also called the main solvent) is mixed with the oil feed and then enters into
an extraction tower, in
which de-asphalted oil and asphalt phase are separated; a second extraction
solvent (it is also called
as auxiliary solvent) is added into the extraction tower bottom to further
extract the asphalt phase, so
as to separate the de-asphalted oil, which is discharged from the top of the
tower. The obtained
de-oiled asphalt phase including extraction solvent is discharged from the
bottom of the tower,
mixed with a dispersing agent and routed to the thermal cracking process. The
first extraction
solvent, the second extraction solvent and the dispersing solvent can be
selected from C3-C6 alkane
or mixed distillates thereof; total mass flow ratio(total mass solvent ratio
to oil feed) of the three
solvents to the feed of the extraction tower is 3-8:1, wherein solvent
distribution proportion is: the
first extraction solvent: the second extraction solvent: the dispersing
solvent is (0.75-0.93): (0-0.15):
0.02-0.10. As the auxiliary solvent is selectively used, when the auxiliary
solvent is used for
extraction, the distribution proportion of three parts of the solvents can be:
the first extraction solvent:
the second extraction solvent; the dispersing solvent is (0.75-0.93) : (0.05-
0.15) : (0.02-0.10.
[0018] As for the solvent deasphalting process, the extraction conditions can
be determined
according to the properties of the heavy oil feedstock and the extraction
solvent, in an embodiment,
the temperature of the extraction tower can be controlled at 80-250 C, and the
extraction pressure
can be controlled at 3.5-10 MPa.
[0019] According to embodiments of the invention, the above mentioned
integrated process also
can include: the de-asphalted oil separated from the solvent deasphalting
process undergoes
adoption of supercritical separation and / or steam stripping to recycle the
extraction solvent
therefrom. The condition of the supercritical separation for recycling the
extraction solvent can be
controlled so that the density of the solvent is 0,15-0.20 g/cm3. The other
feasible means can also be
used for the de-solvent process.
[0020] In an embodiment in the invention, the solvent deasphalting process can
be carried out as
follows: the main solvent and the feed are mixed; the auxiliary solvent is
added through the bottom
of the extraction tower in counter-current contact with the asphalt phase in
the extraction tower to
further enhance the extraction for the asphalt. The solvent used in the
deasphalting process can be
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C3-C6 alkane (comprises paraffin, cycloalkane and olefins) and the mixture
thereof C4-C6 paraffin
or cycloalkane or olefin and the mixture thereof can be used. The solvent in
the de-asphalted oil
phase is recycled after being separated with supercritical separation and then
steam stripping, and
the de-asphalted oil is taken as blending component of the upgraded oil. The
de-oiled asphalt phase
does not need to undergo solvent removal process. After being discharged from
the bottom of the
extraction tower, the de-oiled asphalt phase is mixed with a dispersing agent
that enhances the
dispersion of the de-oiled asphalt, thus resulting in a de-oiled asphalt phase
with good flowability.
[0021] In the process according to an embodiment in the invention, the first
extraction solvent
(main solvent) and the second extraction solvent (auxiliary solvent) are used
for extracting and
separating the heavy oil into the de-asphalted oil and the de-oiled asphalt
phase. The dispersing
solvent is used for enhancing the dispersion of the de-oiled asphalt and
improving its flowability.
Therefore, in theoty, these three solvents can be respectively selected
according to their functions
and effects. In practice, these three solvents can be identical; for example,
all can be C3-C6 alkane
(comprises paraffin or cycloalkane) and the mixture thereof
[0022] As for the technology of deep processing of the heavy oil, in Chinese
invention patents No.
ZL 01141462.6 and No. ZL 200510080799.0, the related American invention patent
No,US
7597797B2, Canada invention patent No. CIP 2,524,995 and French invention
patent No.FR
2888245of the inventors of the invention, a method of deeply separating the
heavy oil is proposed,
With the solvent deasphalting technology, the de-asphalted oil is obtained to
the maximum extent
from the heavy oil. Meanwhile, with coupling technology, the de-oiled asphalt
is subjected to
granulation, thus solving the problems that the asphalt with high softening
point is difficult to be
transported and separated with solvent. In additions, the obtained asphalt
particles can be made into
slurry to be used as fuel or feedstock for synthesis gas produced by
gasification.
[0023] With the further research based on the abovementioned patent in the
prior art, the inventors
of this invention discover that the solvent-containing de-oiled asphalt phase,
without separating the
solvent, can be further mixed with proper dispersing solvent and then directly
introduced into a
thermal cracking reactor, With its good flowability and dispersing properties,
the solvent-containing
de-oiled asphalt phase is dispersed into liquid drops in a thermal cracking
reactor (the de-oiled
asphalt from the extraction tower is dispersed into the thermal cracking
reactor in the form of liquid
drops by mist spray) and mixed with high temperature media, The solvent is
evaporated with heat
from the process, the de-oiled asphalt undergoes thermal reactions to produce
reaction products, thus
not only solving the problem of separation of asphalt from solvent, but also
overcoming the problem
that the asphalt is difficult to be transported because of its flowability,
while through thermal
reaction the conversion of asphalt to light fractions is realized, further
improving the yield of the
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upgraded oil.
[0024] The specific operations of the thermal cracking process technology in
the invention can be
as follows: the de-oiled asphalt including the extraction solvent is dispersed
and injected into a
thermal cracking process reactor, to contact with the heat providing high
temperature media, so as to
obtain thermal cracking products. The heat providing high temperature media
comprises
high-temperature hydrocarbon vapor, high-temperature steam, high-temperature
coke particles
which are partially burned or inorganic particles loaded with burned coke such
as bitumen sand,
quartz sand. The temperature of both the high-temperature hydrocarbon vapor
and the
high-temperature steam can be 500-600 C. The high-temperature coke particles
which are partially
burned or the inorganic particles loaded with burned coke is the coke
discharged from the thermal
cracking reaction or the coke attached to the inorganic particles, which is
recycled back to the
thermal cracking reactor as heat providing media after being burned to 600-750
C.
[0025] According to the integrated process in the invention, the de-oiled
asphalt phase including
the extraction solvent, which is separated from the solvent deasphalting
process, is atomized,
dispersed and injected into the thermal cracking reactor (a reaction tower)
under the action of the
pressure of the extraction tower. Under the action of the dispersing solvent,
the asphalt is dispersed
and then contacts with the high-temperature media to conduct thermal reaction.
The average reaction
temperature of the thermal cracking can be controlled to be 450-550 C, for
example, 470-530 C.
The gas reaction products and the coke are obtained, wherein the coke is
discharged from the bottom
of the reactor. The solvent in asphalt phase is vaporized in the thermal
cracking reaction tower and
then flows out of the top of reaction tower together with the products. The
discharged gas reaction
products arc separated and gas, solvent, thermal cracking oil and 450 C+ heavy
gas oil can be
obtained. The heavy gas oil is recycled and used as the feed of solvent de-
asphalted process, and the
solvents arc recycled back to the solvent deasphalting process to be used.
[0026] The heat providing high-temperature media of the thermal reaction tower
can be obtained
from two ways: one way is the high-temperature steam or high-temperature
hydrocarbon vapor
which is heated to be 500-600 C, and the other way is that the product coke
particles or the coke
loaded on the inorganic particles are partially burned. The temperature of the
produced particles can
be 600-750 C. These particles are recycled back to the thermal reactor and
taken as heat source, so
that the resources can be fully used.
[0027] When the asphalt in the asphalt phase from the solvent deasphalting
process undergoes
thermal reaction in the thermal cracking reactor, at the same time, the
solvent in the asphalt phase is
evaporated and flows out of the tower together with the thermal reaction
products. And then, the
thermal cracking oil, the solvent and the heavy gas oil (it can be regarded as
the heaviest distillate of
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the liquid products of the thermal cracking reaction) can be separated. The
separation method can be
as follows: the thermal cracking reaction products are firstly absorbed by a
heavy oil feedstock;
450 C+ heavy gas oil is separated, and the gas, the solvent and the thermal
cracking oil are further
fractionated and separated. The separated heavy gas oil is recycled back to
the solvent
deasphalting process as the feed and the impurities in the 450 C+ heavy gas
oil, such as asphaltene,
heavy resin and so on are further removed. Furthermore, through further
solvent extraction, the
extractable oil components in the 450 C+ heavy gas oil are separated. The
solvent which is
discharged together with the thermal cracking products is recycled back to the
deasphalting process
for recycle through a specially arranged solvent recycling path. The thermal
cracking oil is obtained
as part of the upgraded oil. Considering the comprehensive factors in the
actual process, when the
thermal cracking reaction products are separated, 450 C+ heavy gas oil (for
example, the distilled
oil with boiling point higher than 450 C-470 C) is controlled to be recycled
back to the solvent
deasphalting process, thus not only being in favor of increasing the total
yield of the oil but also
achieving the purposes of controlling the thermal cracking oil and finally
upgrading the oil quality.
As the oil components have been extracted and separated sufficiently in the
previous process, the
quantity of the heavy gas oil is reduced. Through controlling the flow
quantity of the heavy oil
feedstock that used for absorption, this portion of the distillates can be
stably absorbed and fed back
to the solvent deasphalting process. As for the heavy oil feedstock mentioned
here, it can be obtained
as the heavy oil which is to be processed with the solvent deasphalting
process.
[00281 The obtained distillate oil, the de-asphalted oil and the thermal
cracking oil are mixed
according to the provided proportion, thus obtaining the upgraded oil,
Generally, the distillate oil is
the distillates of light gas oil and straight-run gas oil. According to their
gravity and actual
production, the distillates can be taken as a processed product and directly
stored and transported to
the downstream process for processing. Therefore, in the production, it is
also possible to only mix
the de-asphalted oil and the thermal cracking oil or part of the distillate
oil to form the upgraded oil.
As the undesired components, such as the asphalt with high softening point,
asphaltenes, coke
forming precursors and so on, are removed to the maximum extent with the
integrated process in the
invention, in addition, as the proportions of the straight-run distillate oil
and the extraction oil are
relatively high, the stability of the upgraded oil is significantly increased.
[0029] The upgraded oil provided in the invention can be processed into the
hydro-upgrading oil
with the adoption of the conventional fixed bed hydrotreating process
technology. The operation
difficulty and severity of the hydrotreating process can be obviously reduced,
for example, the
specific operation parameters can be as follows: the temperature of the
hydrotreating process is
360-450 C; the pressure is 6-20MPa, the ratio of hydrogen to oil (volume
ratio) is 200-1200:1, and
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the space velocity of the reactor is 0.3-3.0111.
[0030] In summary, the invention designs and proposes a scientific and
reasonable integrated
process. With the integrated process, the extractable oil components in the
heavy oil is extracted out
without undergoing thermal reaction; the oil components are separated and
collected to the
maximum extent during the physical process, thus beneficial for guaranteeing
the stability of the
upgraded oil products. In addition, as only the residual extracted asphalt is
subjected to the thermal
reaction, thus facilitating the total yields of the coke and the gas to be
lower than those of the process
in the prior art and hence increasing the yield and the quality of the
upgraded oil. In additions, with
the integrated process in the invention, the upgraded oil has relatively
increased API gravity,
significantly reduced carbon residue value, C7 asphaltene and metal content,
the removal of the
asphaltene higher than 96%, and removal of metallic nickel + Vanadium reaches
80-90%. That is,
the undesired components of the heavy oil: the asphalt with high softening
point as well as the
metals, asphaltene and coke forming precursor which arc included in the
asphalt, are removed
significantly, thus the upgraded oil is better meeting the feed specifications
of the conventional
fixed-bed hydrotreating process, facilitating the upgraded oil to be treated
in hydrotreating process to
have relatively high quality and volume yield, and significantly improved
quality.
[0031] With the integrated process in the invention, the heavy oil feedstock
from different sources
can be processed to produce the upgraded oil; for example, if Canada oil sand
bitumen and
Venezuela extra heavy oil which typically have API lower than 10 are
processed, the yields of their
upgraded oils can reach 88.5 wt%(92 v%)and 80.8 wt%(85 v%); the quality of the
upgraded oil can
be improved. Its API gravity can be increased more than 6 units; more than 96%
of C7 asphaltene
can be removed; the residue carbon and metals are significantly reduced, and
the removal of Ni+V
can be 80-90%. The upgraded oil from heavy oil feedstock can be processed
using the conventional
fixed-bed hydrotreating technology, thus significantly reducing the operation
difficulty and severity
of the hydrotreating process and reducing catalyst toxicosis deactivation and
coke forming. As for
the hydrotreating upgraded oil: API is 26; sulfur content is lower than
0.3wt%; asphaltene content is
lower than 0.1wt%, carbon residue is 0.8-2.1wt%, and content of Ni+V are lower
than 3 g/g, thus
meeting the feed specifications of catalytic cracking.
BRIEF DESCRIPTION OF THE DRAWING(S)
[0032] FIG. 1 is a process flow diagram of an example of a integrated process
of processing heavy
oil according to an embodiment of the invention.
[0033] The reference numbers in the drawings can both represent devices and
processes realized
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by the devices: 1: Atmospheric Distillation tower/Atmospheric Distillation; 2:
Vacuum Distillation
Tower /Vacuum Distillation; 3: Extraction Mixer/Mixing; 4: Extraction
Tower/Solvent Deasphalting
Process; 5: Supercritical Solvent Recovery Device/Supercritical Solvent
Recovery; 6: Thermal
Reaction Reactor/Thermal Cracking Reaction; 7: Separator/The Separation Of
Cracking Reaction
Products; 8:, Fixed Bed/Fixed Bed Hydrotreating Process.
DETAILED DESCRIPTION
[0034] With reference to embodiments, the implementation and characteristics
of the invention are
described in details below, so that the spirit and effects of the invention
can be more accurately
understood. The embodiments are exemplary and not intended to limit the
implementation scope of
the invention.
[0035] Referring to FIG I, a integrated process for processing heavy oil
provided in an
embodiment of the invention is described in the followings:
[0036] Prefractionation of the heavy oil feedstock is firstly carried out. It
can be subjected to
atmospheric distillation or atmospheric /vacuum distillation according to the
properties of oil
feedstock, with the cut point temperature of distillates of 350-565 C. The oil
feedstock is distilled in
an atmospheric distillation tower 1 or a vacuum distillation tower 2. The
distillate oil is discharged
from the top of the distillation tower. The substances from the bottom of the
distillation tower are
mixed with a main solvent (an extraction mixer 3 can be arranged here) as feed
material and, then,
enters into an extraction tower 4 to separate de-asphalted oil and asphalt
phase. The asphalt phase is
further extracted by an auxiliary solvent added from the bottom of the
extraction tower 4 if desirable.
The de-asphalted oil which is extracted during the second extraction is
discharged from the top of
the extraction tower. The obtained de-oiled asphalt including the extraction
solvent is discharged
from the bottom of the extraction tower, and mixed with a dispersing solvent
in a transfer pipeline,
and enters into a thermal cracking tower 6 to conduct thermal reaction.
[0037] The prefractionation of the heavy oil feedstock may not be a necessary
step, and whether
conducting the prefractionation depends on the properties of the feedstock.
For example, a heavy oil
feedstock which does not contain lower than 350 C distillate can omit the
prefractionation of
atmospheric distillation /vacuum distillation and be directly subjected to
with the solvent
deasphalting process as the feed material of the extraction tower 4. The other
conditions are that: the
atmospheric distillation 1 and the vacuum distillation 2 also can be
selectively used according to the
properties of the oil feedstock; that is, only the atmospheric distillation,
or only vacuum distillation,
or both of the two processes are carried out.
[0038] The de-oiled asphalt discharged from the bottom of the extraction tower
without separating
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the solvent is directly introduced into thermal cracking 6 after being mixed
with a proper dispersing
solvent. As there is certain pressure in the extraction tower 4, the
discharged asphalt enters into
thermal cracking tower 6 in the form of mist spray. With good flowability and
dispersing properties,
the asphalt is dispersed in the thermal cracking tower 6 (it is also called as
a thermal cracking
reactor) in the form of liquid droplets and mixed with high-temperature media,
with the heat of
which, the de-oiled asphalt undergoes thermal reaction and reaction products
are obtained. The
solvents (comprising extraction solvent and dispersing solvent) entering into
the thermal cracking
tower 6 together with the asphalt are vaporized and flow out of the thermal
cracking tower together
with the thermal reaction products. The coke produced through the thermal
reaction is discharged
from the bottom of the thermal cracking reactor, and the reaction products
flow out of the top of the
thermal cracking tower and are transported into a separator 7 to carry out
heat-exchange condensing
separation. At the same time, part of the heavy oil feedstock (for a process
where atmospheric
distillation/ vacuum distillation is not carried out), or part of substances
from the bottom of the
distillation tower that have been subjected to distillate cut is routed to the
separator 7. The reaction
products are absorbed at the bottom. The circulation amount of the heavy oil
feedstock or the
substances from the distillation bottom of the tower, or directly from the
feedstock is controlled. The
heavy gas oil in the reaction products is separated, circulated, mixed with
the feed material and
recycled back to the extraction tower 4, thus extracting and removing
impurities such as asphaltene,
heavy resin and so on (these impurities enter the thermal cracking tower
together with the asphalt
phase and eventually discharged together with the coke). The oil components
produced in the
thermal reaction are also further extracted into the de-asphalted oil. Gas,
solvent and thermal
cracking oil with the boiling point lower than 450 C are obtained after the
remaining thermal
reaction products further go through heat exchange, condensation and
separation. The gas is
separated and purified, the sulfurous gas (for example, H2S) is recovered as
gas products, and the
purified gas is discharged. The solvent discharged together with the thermal
cracking reaction
products is cooled, separated, discharged out of the separator 7 and recycled
back to the solvent
deasphalting process to be recycled. The thermal cracking oil is discharged
from the bottom of the
separator 7.
[0039] The de-asphalted oil discharged from the top of the extraction tower 4
enters a supercritical
solvent recycling device 5 and undergoes supercritical separation and then
steam stripping to recover
extraction solvent contained therein, and the extraction solvent is recycled
back to the solvent
deasphalting process to be recycled. The supercritical separation with which
the extraction solvent is
recovered is controlled under the condition that the density of the solvent is
0.15-0.20g/cm3. The
ti
CA 02819411 2015-01-15
purpose of the supercritical separation process is to purify the de-asphalted
oil and fully recover the
extraction solvent at the same time.
[0040] The distillate oil, the de-asphalted oil and the thermal cracking oil,
which are formed
through the abovementioned processes, are mixed to form the upgraded oil
provided in the invention.
Compared with the heavy oil feedstock, the API of the upgraded oil is
significantly increased, and
the quality and flowability are greatly improved. According to the design
requirements, the mixed
proportions of the respective oil components can be changed, thus realizing
the flexible adjustment
and control for the upgraded oil. Or the destination of the distillate oil
components can be changed,
thus, part or all of the distillate oil components also can independently be
taken as oil feedstock for
subsequent refining processes and not mixed into the upgraded oil.
[0041] In FIG 1, the upgraded oil obtained through the abovementioned
integrated process also
can be introduced into a fixed bed hydrotreating process 8 so as to obtain
hydrotreating upgraded oil,
[0042] The integrated processes adopted in the following embodiments all can
refer to the
abovementioned processes. According to the requirements of production
objectives and design, the
specific processes and their operating parameters can vary; however, they all
fall within the scope of
the invention and can be understood by those skilled in the art without any
uncertainty.
[0043] Example 1
[0044] Canada Cold Lake oil sand bitumen: API: 10.2; sulfur content: 4.4 wt%;
Conradson
Carbon Residue (CCR): 13.2 wt%; C7 asphaltene: 10.0 wt%; content of Ni and V:
69n/g and 182
[tg/g, respectively.
[0045] The oil sand bitumen is firstly subjected to atmospheric distillation,
200-350 C light gas oil
(15.0 wt%) and substances (residual oil) from the bottom of the atmospheric
tower with boiling
point higher than 350 C are obtained.
[0046] The substances from the bottom of the atmospheric tower undergo a
solvent de-asphalting
process with iso-butane (1C4) as extraction solvent. Firstly, the substances
from the bottom of the
atmospheric distillation tower as feed material are mixed with a main solvent
and fed into an
extraction tower 4 at the middle part or the upper part of the extraction
tower. An auxiliary solvent is
introduced into the extraction tower at the lower part of the extraction tower
and undergoes
countercurrent contact with de-oiled asphalt to enhance extraction to the
asphalt phase which has
been extracted with the main solvent: the temperature at the bottom of the
extraction tower is about
120 C; the temperature at the top of the extraction tower is about 130 C;
extraction pressure is about
4.3MPa. The de-oiled asphalt is mixed with iso-butane (iC4) again as a
dispersing solvent after
12
CA 02819411 2015-01-15
being discharged from the bottom of the extraction tower, thus the asphalt
phase is introduced into a
thermal cracking tower 6 under enhanced dispersing state. During the solvent
deasphalting process,
the ratio of the total mass of solvents to oil feedstock is 4,6:1; the
distribution proportion of the
solvents is: main solvent: auxiliary solvent: dispersing solvent =
0.761:0.217:0.022.
[0047] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly recycled
under supercritical conditions of 4.2 MPa and 160 C (the solvent density is
0.129g/cm3 at this time).
The remaining solvent is further recycled by steam stripping.
[0048] The de-oiled asphalt phase discharged from the extraction tower 4,
containing the extraction
solvent and mixed with the dispersing solvent, is dispersed into the thermal
cracking tower 6 by mist
spray. The fed high-temperature heat providing media is high-temperature steam
with a temperature of
570 C. The average temperature of the thermal cracking reaction is 470 C, at
this time, thermal
reactions of the de-oiled asphalt occur. The formed solid coke is discharged
from the bottom of the
thermal cracking tower 6, the solvent in the asphalt phase together with the
reaction products flow out
form the top of the thermal cracking tower 6 and enters a separator 7.
Meanwhile, a proper amount of
the above mentioned substances from the bottom of the atmospheric tower is
routed into the separator
7, thus heavy gas oil distillate with boiling point higher than 450 C is
absorbed and separated from the
thermal reaCtion products, and recycled back to solvent deasphalting process 4
to be mixed with feed
material and enters the extraction tower 4 to continue extracting and removing
the asphaltene and
heavy resin therein. Gas, solvent and thermal cracking oil with boiling point
lower than 450 C are
obtained after the remaining thermal reaction products are further subjected
to heat exchange,
condensation and separation. The solvent is recycled back to the deasphalting
process 4 to be mixed
with the main solvent and continue being used as solvent. The gas, which is
purified by removing H2S,
is recovered as gaseous product. The thermal cracking oil is led out and mixed
with the light gas oil
distillate obtained from atmospheric distillation and the de-asphalted oil to
obtain upgraded oil, which
serves as oil feedstock for subsequent processing. Through tests, the upgraded
oil has: yield: 81,36
wt% (85,41 v%); API: 18.1; carbon residue: 3.56 wl.%; sulfur content: 3.51
wt%; content of Ni and V:
8.4ug/g and 20.8 ,g/g; yields of by-products gas and coke: 4,95 wt% and 13.68
wt%.
[0049] The upgraded oil may further undergo fixed-bed hydrotreating process 8
under the
conditions: hydrotreating process temperature: 385 C; pressure: 9MPa; hydrogen-
oil ratio (volume
ratio): 600:1; space velocity of the reactor: 2.5 WI. The obtained
hydrotreating upgraded oil has: oil
yield: 78.14 wt% (86,94 v%); API gravity: 27,0; sulfur content: 0.25 wt%;
carbon residue: 1.11 wt%;
asphaltene: <0.05 wt%; content of Ni and V: 0.8ttg/g and 0.9 ng/g,
[0050] Distribution and Properties of Feedstock and Products of Upgraded Oil
Are as Follows:
13
CA 02819411 2015-01-15
Carbon C7Asphaltene
Feedstock S Ni V
API Gravity Residue
wt%(v%) wt% wt% 11g/g. 1,.tg/g
wt%
100 10.2 4.4 13.2 10 65 182
C5+ Oil Yield Products Distribution wt%
wt% Vol% C5-200 C 200-350 C 350-500 C 500 C+
81.36 85.41 4.00 24,49 29.19 42.32
Upgraded Oil _____________________________________________________
Carbon
C7Asphaltene Ni V
API Residue
wt % wt% g/g 11Wg
wt%
18,1 3,51 3,56 0.12 8,4 20.8
Hydrotreating
C5+ Oil Yield Products Distribution wt%
Upgraded Oil
- Initial
wt% Vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
78.14 86.94 17.92 17.70 43.69 20.69
Carbon
C7Asphaltene Ni V
API Gravity Residue
wt% wt% 1-1Wg Pgig
wt%
27.0 0.25 1.11 - <0.05 0.8 0,9
. _
[0051] Through the above integrated processes, the upgraded oil also can be
obtained through
mixing only the thermal cracking oil and the de-asphalted oil, and the
upgraded oil and the light
gas oil distillate from atmospheric distillate are separately stored for
subsequent process, or the
quality of the upgraded oil can also be adjusted and controlled through the
control of proportion of
the light gas oil distillate mixed therein so as to flexibly adjust and
control the increase in API of the
upgraded oil. All of the following examples can be processed in the same way.
[0052] Example 2
[0053] Canada Athabasca oil sand bitumen: API: 8.9; sulfur content: 4.60 wt%;
Conradson
carbon residue (CCR): 13.0%; C7 asphaltene content: 11.03 wt%; content of Ni
and V: 69ngig
and 190 lg/g.
[0054] Through atmospheric distillation, 12.04 wt% of 200-350 C light gas oil
distillate is
14
CA 02819411 2015-01-15
obtained; the yield of substances (residual oil) from the bottom of the
atmospheric tower is 87.96
wt%.
[0055] The substance from the bottom of the atmospheric tower is subjected to
with solvent
de-asphalting process with nC4-nC5 mixed solvent as extraction solvent. The
components of the
extraction solvents are: nC4:nC5-50:50 (wt/wt). The operation of the solvent
deaphalting process is
the same as described in Example 1. However, the mass ratio of the total
solvent to oil feedstock is;
3.95:1; main solvent: auxiliary solvent: dispersing solvent =
0359:0.203:0.038; the temperature at
the bottom of the extraction tower: 140 C; the temperature at the top of the
extraction tower: 160 C;
extraction pressure: 5.0 MPa.
[0056] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly
recovered under supercritical conditions of 4.9MPa and 196 C (the solvent
density is 0.220g/cm3 at
this time). The remaining solvent is further recovered by steam stripping.
[0057] The de-oiled asphalt phase discharged from the extraction tower 4,
containing the extraction
solvent and mixed with the dispersing solvent, is dispersed into a thermal
cracking tower 6 by mist spray.
The thermal cracking reactions occur alter the de-oiled asphalt phase contacts
with 720 C hot coke,
and the average reaction temperature is 490 C. At this time, the de-oiled
asphalt undergoes thermal
reactions, and the product coke is discharged from the bottom of the thermal
cracking tower 6. The
solvent in the asphalt phase together with the reaction products flows out of
the top of the then-nal
cracking tower 6 and enters into a separator 7. Meanwhile, appropriate amount
of the abovementioned
substances from the bottom of the atmospheric tower is routed to the separator
so as to facilitate heavy
gas oil with boiling point higher than 450 C to be absorbed and separated from
the thermal reaction
products, and recycled back to solvent deasphalting process 4 to be mixed with
feed materials, and enters
into the extraction tower 4. The gas, solvent and thermal cracking oil with
boiling point lower than
450 C are obtained after the remaining thermal reaction products being
distilled and separated. The gas,
which is purified by removing I-12S, is recovered. The solvent is recycled
back to the &asphalting
process and continues to be used as solvent (it can be used as main solvent,
auxiliary solvent and / or
dispersing solvent). The thermal cracking oil is led out and mixed with the
above light gas oil distillate
and the de-asphalted oil to obtain the upgraded oil. With the tests, the
upgraded oil is: oil yield: 84,07
wt% (88.64 v%) ; API gravity: 16.5; carbon residue: 4,71 wt%; sulfur content:
3.55 wt%; content of Ni
and V: 12.9 g/g and 29.3ng/g. Yields of the by-products gas and the coke: 4.15
wt% and 11.78 wt%.
[0058] The abovementioned upgraded oil is further undergo with fixed-bed
hydrotreating process
8 and hydrotreating upgraded oil can be obtained, wherein the hydrotreating
process is conducted
under the conditions: temperature: 395 C; reaction pressure: 10 MPa; hydrogen-
oil ratio (volume
CA 02819411 2015-01-15
ratio): 600:1; space velocity of the reactor; 1.8 ; the yield of
hydrotreating upgraded oil: 80.79
wt%(90.44 v%); API gravity: 25.7; sulfur content: 0.23 wt%; carbon residue:
1.71 wt%; asphaltene:
<0.05 wt%; content of Ni and V: 1.1ug/g and 0,9 ug/g.
[0059] Distribution and Properties of Raw Material and Products of Upgraded
Oil Are as Follows;
Carbon V
Feedstock API C7Aspha Ni
S wt% Residue 1-lg
wt%(v%) Gravity ltene ng/g
wt% /g
wt%
19
100 8.9 4.6 13 11.03 65.4
2.6
C5+ Oil
Products Distribution wt%
Yield
wt vol Initial Boiling 350-500 500
200-350 C
% % Point-200 C C C+
Upgraded Oil 84, 88. 40.4
2.30 17.36 39.94
07 64 0
Carbon C7Aspha V
Ni
API Residue Itene p,g/
wt% 1-Lgig
wt% wt%
29.
16.5 3.55 4.71 0,14 12,9
3
Hydrotreating C5+ Oil
Products Distribution wt%
Upgraded Oil Yield
wt vol Initial Boiling 350-500 500
200-350 C
% % Point-200 C C C+
80. 90. 19.7
13,72 15.64 50.88
79 44 6
Carbon C7Aspha V
API Ni
S wt% Residue ltenc
= Gravity 1.1g/g
wt% wt%
25,7 - 0.23 1.71 <0.05 1.1 0.9
[0060] Example 3
[0061] Canada Athabasca oil sand bitumen: API: 8.9; sulfur content: 4.6 wt%;
Conradson
carbon residue (CCR): 13.0%: C7 asphaltene content: 11.4 wt%; content of Ni
and V: 65,4[1g/g
16
CA 02819411 2015-01-15
=
and 192.6 ug/g.
[0062] Through atmospheric and vacuum distillation, 12.04 wt% of 200-350
Clight gas oil
distillate and 32.75 wt% of 350-500 C straight-run gas oil are obtained; the
yield of the substances
from the bottom of a vacuum tower (residual oil with boiling point higher than
500 C) is 55.21 wt%.
[0063] The residual oil from the bottom of the vacuum tower is subjected to
deasphalting process
with n-pentane (nC5) being used as extraction solvent. The specific operation
is as described in
Example 1, The mass ratio of total solvent to oil feedstock is 3.7:1, wherein
the main solvent:
auxiliary solvent: dispersing solvent is 0,811:0.135:0.054; the temperature of
the bottom of the
extraction tower: 160 C; the temperature of the top of the tower: 170 C;
extraction pressure: 5,5
MPa.
[0064] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly
recovered under supercritical conditions of 5.4 MPa and 240 C (the solvent
density is 0.196g/cm3 at
this time). The remaining solvent is further recovered by steam stripping.
[0065] The de-oiled asphalt phase, discharged from the extraction tower 4,
including the extraction
solvent and mixed with dispersing solvent, is dispersed into a thermal
cracking tower 6 by mist spray.
The thermal cracking reactions occur after the de-oiled asphalt phase contacts
with 700 C thermal
bitumen sand, The average temperature of the reaction reaches 500 C. At this
time, the de-oiled
asphalt undergoes thermal reaction, and the formed solid coke is discharged
from the bottom of a
thermal cracking tower 6. The solvent in the asphalt phase together with the
reaction products flow
out of the top of the thermal cracking tower 6 and is introduced into a
separator 7. Meanwhile,
appropriate amount of the abovementioned substances from the bottom of the
vacuum tower is
routed to the separator so as to facilitate heavy gas oil with boiling point
higher than 470 C to be
absorbed and separated from the thermal reaction products, and recycled back
to solvent
deasphalting process 4 to be mixed with feed, and entered into the extraction
tower 4 to be extracted
continuously. The gas, solvent and thermal cracking oil with boiling point
lower than 470 C are
obtained after the remaining thermal reaction products are further distilled
and separated. The gas,
which is purified by removing H2S, is recovered. The solvent is recycled back
to the deasphalting
process 4 and continues to be used as solvent. The thermal cracking oil is led
out and mixed with the
above light gas oil distillate and the de-asphalted oil to obtain upgraded
oil. Through tests, the
upgraded oil: yield: 86.62 wt%(90.4 v%); API: 15.0; carbon residue: 4,91 wt%;
sulfur content: 3.73
wt%; content of Ni and V: 16,9 ug/g and 46.5 ug/g; yields of gas and coke
which are by-products:
3.07 wt% and 10,3 wt%.
[0066] The abovementioned upgraded oil is further subjected to fixed-bed
hydrotreating process 8
and hydrotreating upgraded oil can be obtained. The hydrotreating process is
conducted under the
17
CA 02819411 2015-01-15
conditions: temperature: 400 C; reaction pressure: 11 MPa; hydrogen-oil ratio
(volume ratio): 800:1;
space velocity of its reactor: 1.5 11-1. The obtained hydrotreating upgraded
oil: yield: 83.41 wt%
(93.80 v%); its API gravity: 26.4; sulfur content: 0.24 wt%; carbon residue:
1.78 wt%; asphaltene:
0.08 wt%; content of Ni and V: 0.8 g/g and 1.4 g/g.
[0067] Distribution and Properties of Raw Material and Products of Upgraded
Oil Are as Follows:
Carbon C7Asphal V
Feedstock Ni
API Gravity Residue tene
wt%(v%) wt% ug/g
wt% wt%
192
100 8,9 4.6 13 11.4 65.4
.6
C5+ Oil Yield Products Distribution, wt%
Vol Initial Boiling 350-500 500
wt% 200-350 C
% Point-200 C C C+
90.4 40.5
Upgraded Oil 86,62 0 2.49 17.66 39.31
4
Carbon C7Asphal V
Ni
API Residue tene ug,/
wt.% ug/g
wt% wt%
46.
15,0 3.73 4.91 0.25 16.2
Hydrotreating C5+ Oil
Products Distribution wt%
Upgraded Oil Yield
Vol Initial Boiling 350-500 500
wt% 200-350 C
% Point-200 C C C+
93.8 19.7
83,41 13,53 15.72 51.00
0 6
Carbon C7Asphal V
Ni
APIGRAVITY Residue tene ug/
wt% 1..tg/g
wt% wt%
26.4 0.24 1,78 0.08 1.5 1.4
[0068] The atmospheric and vacuum distillation oil (light gas oil distillates
and straight-run
vacuum gas oil ), which are obtained through the aboveinentioned integrated
process, also can be
stored independently and used as feed in subsequent process, or mixed with
thermal cracking oil in
controlled proportion according to requirements to become the upgraded oil.
18
CA 02819411 2015-01-15
[0069] Example 4
[0070] Canadian oil sand bitumen, which has the same properties as that of
Exaniple 3.
[0071] The oil sand bitumen is firstly subjected to atmospheric and vacuum
distillation, and 12.04
wt% 200-350 C light gas oil distillate ; 28.75 wt% of 350-524 C straight-run
vacuum gas oil are
obtained; the yield of the substances from the bottom of the vacuum tower
(vacuum residual oil) is
50.5 wt%.
[0072] With the mixed solvent of n-pentane (nC5) and cyclopentane being used,
VTB is subjected
to a deasphalting process. The specific operation is as described in Example
1. The composition of
extraction solvent is; n-pentane cyclopentane is 0.9 (w0:0.1(wt), the mass
ratio of the total solvent
to oil feedstock is 4.3;1, wherein the main solvent: auxiliary solvent:
dispersing solvent --
0.698:0.233:0.070; the temperature of the bottom of the extraction tower: 160
C; the temperature of
the top of the tower: 170 C; extraction pressure: 5.5 WIPa.
[0073] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly recycled
under supercritical conditions of 4.85MPa and 230 C (the solvent density is
0.195g/cm3 at this time).
The remaining solvent is further recycled by steam stripping.
[0074] The de-oiled asphalt phase, discharged from the extraction tower 4,
including the extraction
solvent and mixed with dispersing solvent, is dispersed into a thermal
cracking tower 6 by mist spray.
The temperature of the de-oiled asphalt reaches 505 C after it contacts with
hot coke, and then
thermal reaction occurs to produce reaction products. The produced solid coke
is discharged from
the bottom of a thermal cracking tower 6. The solvent in the asphalt phase
together with the reaction
products flow out of the top of the thermal cracking tower 6 and into a
separator 7. Meanwhile,
appropriate amount of the abovementioned substances from the bottom of the
tower is routed to the
separator 7 so as to facilitate heavy gas oil with boiling point higher than
500 C to be absorbed and
separated from the thermal reaction products, and recycled back to solvent
deasphalting process 4 to
be mixed with residual oil feed, and entered into the extraction tower 4 to be
extracted continuously.
The gas, solvent and thermal cracking oil with the boiling point lower than
500 C are obtained after
the remaining thermal reaction products are further distilled and separated.
The gas, which is
purified by removing 1-12S, is recovered. The solvent is recycled back to the
deasphalting process 4
and continues to be taken as solvent. The upgraded oil is obtained through
mixing the thermal
cracking oil, straight-run light gas oil and vacuum gas oil and the de-
asphalted oil. Through tests, the
upgraded oil: yield; 88.54 wt%(91,96 v%); API: 14.3; carbon residue: 5.71 wt%;
sulfur content: 3.84
wt%; content of Ni and V: 20.0ug/g and 57.9ug/g; yields of by-products gas and
coke: 2.48 wt%
19
CA 02819411 2015-01-15
and 8.98 wt%.
[0075] The above upgraded oil is further subjected to fixed-bed hydrotreating
process 8 and the
hydrotreating upgraded oil is obtained. The hydrotreating process is conducted
under the conditions:
temperature: 400 C; reaction pressure: 13 Mpa; hydrogen-oil ratio (volume
ratio): 1000:1; space
velocity of reactor: 1.0 h. The obtained hydrotreating upgraded oil: yield:
85.16 wt% (95.46 v%);
API gravity: 25.9; sulfur content: 0.26 wt%; carbon residue: 2.08 wt%;
asphaltene: 0.08 wt%;
content of Ni and V: 1.54g/g and 1.2 pg/g.
[0076] Distribution and Properties of Raw Material and Products of Upgraded
Oil Are as Follows:
Carbon C7Asphaltene
Feedstock S Ni V
API Gravity Residue
wt%(v%) wt% wt% itg/g lig/g
wt%
100 8.9 4,6 13 11.4 65.4 192.6
C5+ Oil Yield Products Distribution wt%
Initial
wt% Vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
Upgraded Oil
88,54 91.96 1.86 16.34 38.15 43.65
Carbon
C7Asphaltene Ni V
API Gravity Residue
wt% wt% ugig
wt%
14.3 184 5,71 0.27 20.0 57.9
Hydrotreating C5+ Oil Yield Products Distribution wt%
Upgraded Oil
Initial
wt% Vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
85,16 95.46 12.90 15.04 50.76 21.30
Carbon
C7Asphaltcne Ni V
API Gravity Residue
wt% wt% [ig/g pg/g
wt%
-25,9 0.26 2.08 0.08 1.5 1.2
[0077] Example 5
[0078] Venezuela extra heavy oil : API: 8.7; sulfur content; 4.0 wt%;
Conradson carbon residue
CA 02819411 2015-01-15
(CCR): 15.1%; the content of Ni and V: 111g and 487 g/g.
[0079] The extra heavy oil is firstly subjected to atmospheric and vacuum
distillation, and 11.24
wt% of 200-350 C light gas oil distillate ; 23,44 wt% of 350-524 C vacuum gas
oil distillate
are obtained; the yield of the substances from the bottom of the vacuum tower
with boiling point
higher than 500 C is 65.32 wt%.
[0080] With n-pentane (nC5) being used as extraction solvent, the substances
from the bottom of
the vacuum tower is subjected to deasphalting process. The specific operation
is as described in
Example 1. The mass ratio of total solvent to oil feedstock; 4:1, wherein the
main solvent: auxiliary
solvent: dispersing solvent = 0,714;0.238:0.048; the temperature of the bottom
of the extraction
tower: 170 C; the temperature of the top of the tower: 180 C; extraction
pressure: 5.0 MPa,
[0081] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly
recovered under supercritical conditions of 4.9 MPa and 250 C (the solvent
density is 0.170g/cm3 at
this time). The remaining solvent is further recovered by steam stripping.
[0082] The de-oiled asphalt phase, discharged from the extraction tower 4,
including the
extraction solvent and mixed with dispersing solvent, is dispersed into a
thermal cracking tower 6 by
mist spray. The temperature of the de-oiled asphalt reaches 500 C after
contacting with hot coke,
and then thermal reaction occurs to produce reaction products. The produced
solid coke is
discharged from the bottom of the thermal cracking tower 6. The solvent in the
asphalt phase
together with the reaction products flow out of the top of the thermal
cracking tower 6 and is
introduced into a separator 7. At the same time, appropriate amount of the
above substances from
the bottom of the tower is routed to the separator 7 so as to facilitate heavy
gas oil with boiling point
higher than 470 C to be absorbed and separated from the thermal reaction
products, and recycled
back to solvent deasphalting process 4 to be Mixed with feed and continue to
be extracted. The gas,
solvent and thermal cracking oil with the boiling point lower than 470 C are
obtained after the
remaining thermal reaction products being distilled and separated. The gas,
which is purified by
removing H2S, is recovered. The solvent is recycled back to the deasphalting
process 4 and
continues to be used as solvent. The upgraded oil is obtained through mixing
the thermal cracking
oil, vacuum gas oil distillate and the de-asphalted oil. Through tests, the
upgraded oil: yield: 80,83
wt% (84.94 v%); API; 16.0; carbon residue; 4,11 wt%; sulfur content: 3.23 wt%;
content of Ni and
V: 9.611g/g and 41.9n/g; the yields of by-products gas and coke: 4,67 wt% and
14.5 wt%.
[0083] The above upgraded oil is further subjected to fixed-bed hydrotreating
process 8 and the
hydrotreating upgraded oil is obtained. The hydrotreating process:
temperature: 400 C; reaction
pressure: 15.0Mpa; hydrogen-oil ratio (volume ratio); 1200:1; space velocity
of reactor; 1,0 11.1.
21
CA 02819411 2015-01-15
The obtained hydrotreating upgraded oil: yield; 78.20 wt% (88.31 v%); API
gravity: 27.1; sulfur
content: 0.19 wt%; carbon residue: 0.80 wt%; asphaltene<0.05 wt%; content of
Ni and V: 0.54g
and 1.0
[0084] DiStribution and Properties of Feedstock and Products of Upgraded Oil
Are as Follows:
Carbon C7Asphaltene
Feedstock S Ni
API Gravity Residue
wt%(v%) wt% wt% ytg/g ug/g
wt%
100 8.7 4.0 15.1 9.5 80 410
C5+ Oil Yield Products Distribution wt%
Initial
wt% Vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
Upgraded Oil
80.83 84.94 4.31 20.14 31.92 43.64
Carbon
C7Asphaltene Ni
API Gravity Residue
wt% wt% igIg eg
wt%
16.0 3.23 4.11 0.19 9.6 41.9
I Iydrotreating
C5+ Oil Yield Products Distribution wt%
Upgraded Oil
Initial
wt% Vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
- 78.20 88.31 14,66 16.88 47.29 21.17
Carbon
C7Asphaltene Ni V
API Gravity Residue
wt% wt% 1.tg/g Rig
wt%
27.1 0.19 0.80 <0.05 0.5 1.0
[0085] Example 6
[0086] Indonesia Buton Island oil sand bitumen : API: 7.8; sulfur content:
6.67 wt%; Conradson
carbon residue (CCR): 17.5%; the content ofNi and V: 47.5 g/g and 144 ug/g.
[0087] With atmospheric distillate and 350 C of cut point, 6.49 wt% or 200-350
C light gas oil
distillate is obtained.
[0088] The mixed solvent of n-pentane and n-hexane (n-pentane/n-hexane =
80:20) is used as
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CA 02819411 2015-01-15
extraction solvent and the substances from the bottom of the atmospheric
distillation tower is
subjected to deasphalting process. The specific operation is as described in
Example 1.The mass
ratio of total solvent to oil feedstock is 3.7:1, wherein the main solvent:
auxiliary solvent : dispersing
solvent = 0,676:0.270:0.054; the temperature of the bottom or the extraction
tower: 160 C; the
temperature of the top of the tower: 180 C; extraction pressure: 6.0 MPa.
[0089] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly
recovered under supercritical conditions of 5.85 MPa and 260 C (the solvent
density is 0.200g/cm3
at this time).. The remaining solvent is further recovered by steam stripping.
[0090] The de-oiled asphalt phase, discharged from an extraction tower 4,
including the extraction
solvent and mixed with dispersing solvent, is dispersed into a thermal
cracking tower 6 by mist spray.
After contacting with 680 C hot coke particles, the temperature of the de-
oiled asphalt reaches
500 C, and then the thermal reaction occurs to produce reaction products. The
produced solid coke
is discharged from the bottom of the thermal cracking tower 6. The solvent in
the asphalt phase
together with the reaction products flow out of the top of the thermal
cracking tower 6 and is
introduced into a separator 7. At the same time, appropriate amount or the
substances from the
bottom of the abovementioned tower is routed to the separator 7 so as to
facilitate heavy gas oil
with boiling point higher than 470 C to be absorbed and separated from the
thermal reaction
products, and recycled back to deasphalting process 4 to be mixed with feed
and continue to be
extracted. The gas, solvent and thermal cracking oil with the boiling point
lower than 470 C am
obtained after the remaining thermal reaction products are distilled and
separated. The gas, which is
purified by removing II2S, is recovered, The solvent is recycled back to the
deasphalting process and
continues to be used as solvent. The upgraded oil is obtained through mixing
the thermal cracking -
oil, light gas oil distillate and the de-asphalted oil. Through tests, the
upgraded oil: yield: 79,30 wt%
(83.04 v%); API: 15.2; carbon residue: 5.05 wt%; sulfur content: 6.55 wt%;
content of Ni and V:
8.14ng and 23.65 g/g; the yields of by-products gas and coke: 4.77 wt% and
15.93 w/o.
[0091] The above upgraded oil is further subjected to fixed-bed hydrotreating
process 8 and
hydrotreating upgraded oil can be obtained, wherein the hydrotreating process
is conducted under
the conditions: temperature: 400 C; reaction pressure: 15 MPa; hydrogen-oil
ratio (volume ratio):
1000:1; the space velocity of reactor: 0.8 h`l. The obtained hydrotreating
upgraded oil: yield: 75.60
wt% (85.26 v%); API gravity: 26.5; su content: 0.31 wt%; carbon residue:
1.85 wt%; asphaltene:
0.07 wt%; content of Ni and V: 0.7ng/g and 1,2 ng/g.
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[0092] Distribution and Properties of Raw Material and Products of Upgraded
Oil Are as Follows:
Carbon C7Asphaltene
Feedstock S Ni V
API Gravity Residue
wt /0(V/0) wt% wt% ng/g ng/g
wt%
100 7.8 6.67 17.5 12.9 47.5 144
C5+ Oil Yield -Products Distribution wt%
Initial
, wt% vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
Upgraded Oil _
79.30 83,04 4.24 14,58 41.90 39.28
Carbon
C7Asphaltene Ni V
API Gravity Residue
wt% wt% ng/g 1-Leg
wt%
15.2 6,55 5.05 0,23 8.14 23,65
Hydrotreating
C5+ Oil Yield Products Distribution wt%
Upgraded Oil
Initial
wt% vol% Boiling 200-350 C 350-500 C 500 C+
Point-200 C
75.60 85,26 10,77 16.28 53.62 19.34
Carbon
C7Asphaltene Ni V
API Gravity Residue
wt% wt% ng/g lAgig
wt%
26,50 0.31 1.85 0.07 0.7 1,2
[0093] The light gas oil distillates and upgraded oil, obtained through the
above integrated process,
also can be stored respectively and used as oil feedstock in the subsequent
process.
[0094] Example 7
[0095] China Inner Mongolia oil sand bitumen: API: 7.8; sulfur content: 1.0
wt%; Conradson
carbon residue (CCR): 17.4%; C7 asphaltene content: 27.2 wt%; the content of
Ni: 16 g/g.
[0096] As the oil sand bitumen does not include distillate with the
temperature less than 350 C, the
mixed solvent of n-pentane and n-hexane (n-pentane/n-hexane = 90:10) is
directly used as extraction
solvent and the oil sand bitumen is subjected to deasphalting process. The
specific operation is as
described in Example 1. The mass ratio of total solvent to oil feedstock is
4.3:1, wherein the main
solvent: auxiliary solvent : dispersing solvent = 0.733:0.222:0.044; the
temperature of the bottom of
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CA 02819411 2015-01-15
the extraction tower: 160 C; the temperature of the top of the tower: 170 C;
extraction pressure: 5.8
MPa.
[0097] The solvent in the de-asphalted oil discharged from the extraction
tower 4 is firstly recycled
under supercritical conditions of 5.7 MPa and 240 C (the solvent density is
0.234Wcm3 at this time).
The remaining solvent is further recycled by steam stripping.
[0098] The de-oiled asphalt phase, discharged from an extraction tower 4,
including the extraction
solvent and mixed with dispersing solvent, is dispersed into a thermal
cracking tower 6 by mist spray.
After contacting with 680 C hot coke particles, the temperature of the de-
oiled asphalt reaches
500 C, and then thermal reaction occurs to produce reaction products. The
produced solid coke is
discharged from the bottom of the thermal cracking tower 6. The solvent in the
asphalt phase
together with the reaction products flow out of the top of the thermal
cracking tower 6 and is
introduced into a separator 7. At the same time, appropriate amount of oil
feedstock is routed to
the separator 7 so as to facilitate heavy gas oil with boiling point higher
than 450 C to be absorbed
and separated from the thermal reaction products, and recycled back to
deasphalting process 4 to be
mixed with, oil feedstock and continue to be extracted. The gas, solvent and
thermal cracking oil
with the boiling point lower than 450 C are obtained after the remaining
thermal reaction products
are distilled and separated. The gas, which is purified by removing 1-12S, is
recovered. The solvent is
recycled back to the deasphalting process and continues to be used as solvent.
The upgraded oil is
obtained through mixing the obtained thermal cracking oil and the de-asphalted
oil. The upgraded
oil: yield: 72.65 wt% (76.52 v%); API: 16.1; carbon residue: 5.51 wt%; sulfur
content: 0.74 wt%;
the content of Ni: 3.0]tg; the yields of by-products gas and coke: 7.9 wt% and
19.45 wtcY0.
[0099] Distribution and Properties of Feedstock and Products of Upgraded Oil
Are as Follows:
Carbon C7Asphaltenc
Feedstock S Ni
API Gravity Residue
wt%(v%) wt% wt% ug/g
wt%
100 7.8 1.0 17.4 27.2 16
C5+ Oil Yield Products Distribution wt%
Initial Boiling
wt% Vol% 200-350 C 350-500 C 500 C+
Point-200 C
Upgraded 72.65 76.52 9.88 16.19 25.10 48.83
Oil Carbon
C7Asphaltene Ni
API Gravity Residue
wt% wt%
wt%
16.1 0.74 5.51 0.94 3.0
=
